CN113698003B - System and method for refining vanadium-chromium-titanium waste salt for chlor-alkali - Google Patents
System and method for refining vanadium-chromium-titanium waste salt for chlor-alkali Download PDFInfo
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
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- C02F9/00—Multistage treatment of water, waste water or sewage
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- C02F1/20—Treatment of water, waste water, or sewage by degassing, i.e. liberation of dissolved gases
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- C—CHEMISTRY; METALLURGY
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- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/442—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by nanofiltration
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- C—CHEMISTRY; METALLURGY
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Abstract
The invention discloses a system and a method for refining vanadium-chromium-titanium waste salt for chlor-alkali, wherein the refining system comprises a water distribution barrel, the water distribution barrel is sequentially connected with a pipeline mixer, a gas-liquid separator and a salt dissolving tank, the salt dissolving tank is connected with a titanium filter screen, the titanium filter screen is sequentially connected with a baffling tank, a primary reaction tank, a filtering head tank, a primary filter and a liquid inlet buffer tank, the liquid inlet buffer tank is sequentially connected with a primary heat exchanger, a secondary heat exchanger, a chlorate decomposer and a secondary reaction tank, the secondary reaction tank is sequentially connected with a coarse filter and a secondary filter, the coarse filter and the secondary filter are both connected with a secondary deslagging tank, the secondary deslagging tank is connected with a secondary plate-and-frame filter press, and the primary filter and the primary heat exchanger are both connected with a primary deslagging tank. The invention also comprises a using method of the system. The method recycles the waste vanadium, chromium and titanium salt in the production process of chlor-alkali, and effectively solves the technical problems that the removal of heavy metals such as vanadium, chromium, titanium and the like and chlorate ions is difficult and the industrial production is difficult.
Description
Technical Field
The invention belongs to the technical field of waste water and waste salt treatment, and particularly relates to a system and a method for refining vanadium, chromium and titanium waste salt for chlor-alkali.
Background
In recent years, titanium production enterprises (titanium sponge and titanium dioxide by chlorination process) promote the reduction of waste and secondary resource sources, clean and environment-friendly production, introduce a wastewater treatment system and a waste residue treatment system, and respectively treat salt-containing waste liquid produced by a tail gas treatment system of each process and salt-containing furnace slag discharged by a molten salt chlorination furnace. High-salinity wastewater mainly containing sodium chloride is generated, and solid waste salt (NaCl) is obtained after concentration, evaporation, centrifugal separation and drying. Because the vanadium, chromium and titanium solid waste salt contains low sodium chloride (less than or equal to 93 percent), the waste salt formed by the two processes has the characteristics of different components, high content of harmful impurities, more components, complex form and the like, the vanadium, chromium and titanium solid waste salt cannot be completely reused for a molten salt chlorination furnace, has limited export sales uses, and cannot be buried, so that the disposal of the redundant solid waste salt is difficult. Becomes the difficult problem of 'neck' facing the development of titanium enterprises and needing to be solved urgently.
The application of the solid waste salt in the chlor-alkali industry is a recommended optimal waste salt resource utilization mode. However, the waste salt produced by titanium enterprises is abundant in metal cations with different valence states and anions such as sulfate radical and chlorate radical, and the impurities just have important influence on the ion membrane electrolysis production process in chlor-alkali chemical industry, such as the increase of the voltage of an electrolysis cell, the reduction of current efficiency, and even cause the damage of an ion membrane to cause safety accidents. Therefore, the waste salt produced by titanium enterprises is recycled for chlor-alkali production, which has the disadvantages of high technical difficulty, high disposal cost and high risk, and is unacceptable for most chlor-alkali enterprises.
Disclosure of Invention
Aiming at the defects, the invention provides a system and a method for refining waste vanadium, chromium and titanium salt for chlor-alkali, which can reduce the content of heavy metals such as vanadium, chromium, titanium and the like and the content of chlorate in the waste salt, and effectively solve the technical problems of difficult removal of heavy metals such as vanadium, chromium, titanium and the like and chlorate ions and difficult industrial production by reusing the produced waste salt in the production process of chlor-alkali.
In order to achieve the purpose, the technical scheme adopted by the invention for solving the technical problems is as follows: the utility model provides a vanadium chromium titanium waste salt refining system for chlor-alkali, including the distribution bucket, the distribution bucket and pipeline mixer, vapour and liquid separator and salt dissolving pond are connected in order, the salt dissolving pond is connected with the titanium filter screen, the titanium filter screen is with the baffling groove, the one-level reaction pond, filter the elevated tank, one-level filter and feed liquor dashpot are connected in order, one-level filter still is connected with the one-level reaction pond, the feed liquor dashpot is connected with one-level heat exchanger, the second grade heat exchanger, chlorate decomposer and second grade reaction pond are connected in order, the second grade heat exchanger still is connected with baffling groove and second grade reaction pond respectively, chlorate decomposer still is connected with the one-level heat exchanger, the second grade reaction pond still is connected with the feed liquor dashpot, the second grade reaction pond is connected with coarse filter and second grade filter in order, coarse filter and second grade filter all are connected with second grade row sediment pond, second grade row sediment pond is connected with second grade plate and frame filter press, one-level filter and one-level heat exchanger all are connected with the distribution bucket.
The using method of the vanadium, chromium and titanium waste salt refining system for chlor-alkali adopts a two-step method to remove vanadium, chromium and titanium, and comprises the steps of adding a refining agent AB and a pH stabilizer, and converting high-valence ions into low-valence ions or removing the high-valence ions by flocculation precipitation and filtration at a low pH value in the conversion process of the pH value from low to high; then, the flocculated hydroxide precipitate is filtered to further remove the water under neutral or weak alkaline.
Further, the use method of the vanadium-chromium-titanium waste salt refining system for chlor-alkali comprises the following steps: high-salinity wastewater and other salt dissolving water are mixed by a water distribution barrel to form salt dissolving water, hydrochloric acid is added to adjust the pH value, the salt dissolving water enters a salt dissolving tank to dissolve solid waste salt to obtain vanadium-chromium-titanium saturated salt water, then hydrochloric acid and a refining agent AB are added to be mixed, the mixture enters a primary reaction tank, a pH stabilizing agent is added to the primary reaction tank to maintain a low pH value, and the mixture is stirred and mixed to complete primary refining reaction; filtering the brine after the primary refining reaction by a primary filter, adding hydrochloric acid and a chlorate decomposer, then feeding into a chlorate decomposer, and heating by steam to maintain the reaction temperature to complete the decomposition of chlorate; the first-stage refined salt water with low chlorate content enters a second-stage reaction tank, a pH stabilizer is continuously added into the second-stage reaction tank to maintain a high pH value, and the first-stage refined salt water and the second-stage refined salt water are mixed to complete a second-stage refining reaction; and filtering the brine after the secondary refining reaction by a secondary refining filter to obtain qualified brine, and entering a chlor-alkali brine refining system for continuously removing impurities.
Further, the pH value of the salt solution is 6.5-7.5, the pH value of the salt solution is 1.5-2.5 after hydrochloric acid and a refining agent AB are added into the first-stage reaction tank, the pH value of the salt solution is 2.5-5 after a pH stabilizing agent is added into the first-stage reaction tank, and the pH value of the salt solution is 7-9 after a pH stabilizing agent is added into the second-stage reaction tank.
Further, the reaction temperature in the chlorate decomposer is 80-95 ℃, and the pH value is 1.5-2.5.
Further, the chlorate decomposer is at least one of sodium thiosulfate, formaldehyde, acetaldehyde and glyoxal.
Further, the refining agent AB is at least one of ferric nitrate, ferrous chloride, ferric trichloride, ferric sulfate, ferrous sulfate, ferric tribromide, ferrous bromide and ferric perchlorate.
Further, the pH stabilizer comprises the following components in parts by mass: 5-7 parts of methyl alcohol amine, 1-3 parts of sodium hydroxide and 1-3 parts of sodium bicarbonate.
Furthermore, the qualified salt contains 290-310g/L of sodium chloride, less than or equal to 0.01mg/L of vanadium, chromium and titanium, less than or equal to 0.02mg/L of other heavy metal ions and less than or equal to 5g/L of chlorate radical.
Furthermore, the impurities can be removed more thoroughly by utilizing reflux regulation of different flow rates, the addition of a refining agent is saved, the steam consumption is reduced, and the production cost is reduced. The flow of the salt solution in the evolved salt pond is slightly larger than that of the salt solution in the secondary filter (a small amount of salt solution enters the slag pond through slag discharge), and the flow of the salt solution in the elevated tank of the primary filter is 1.5-2.0 times of that of the salt solution in the evolved salt pond; the brine flow of the chlorate feed decomposer is smaller than the brine flow of the secondary filter (partial decomposition).
Further, the first-stage filtration adopts an organic membrane micro-pressure terminal filtration process, and the membrane aperture is 300-400nm; the secondary filtration adopts inorganic membrane pressure cross flow filtration technology, the filtration pressure is 200-300Kpa, and the membrane aperture is 40-50nm. Therefore, the refining agent AB still remained in the secondary reaction liquid can be ensured to play a role in flocculation, and the full secondary refining reaction and the more reliable indexes of qualified saline water after secondary filtration can also be ensured.
In summary, the invention has the following advantages:
1. the vanadium, chromium and titanium waste salt is used in the production process of chlor-alkali, heavy metal ions such as vanadium, chromium, titanium and the like and chlorate ions which have great influence are concentrated in a vanadium, chromium and titanium waste salt refining system and are synchronously removed; not only reduces the production cost, but also lightens the impurity removal load of the subsequent chlor-alkali brine refining system.
2. A method for removing heavy metals such as vanadium, chromium, titanium and the like by two-step refining reaction filtration is adopted, and by utilizing the characteristic that ions with different valence states form precipitates under different pH values, the heavy metals such as vanadium, chromium, titanium and the like are removed more completely, the indexes are easier to control, vanadium, chromium and titanium in the treated brine are respectively less than or equal to 0.01mg/L, and other heavy metal ions are less than or equal to 0.02mg/L (note: the indexes of calcium, magnesium and iron are not included).
3. The removal of chlorate is more complete. The high-temperature hydrochloric acid decomposition method with chlorate decomposer is adopted, the decomposition rate of chlorate is more than or equal to 85 percent, chlorate in the brine returned to the chlor-alkali brine refining system is less than or equal to 5g/L, and the load of a chlorate decomposition device in the chlor-alkali brine refining system cannot be increased. The residual decomposing agent is removed under the action of trace titanium dioxide in the secondary refining reaction, and cannot be brought into a subsequent system.
4. Two-step filtration is carried out by adopting different membrane filtration processes. The first-stage refining filtration adopts an organic membrane micro-pressure terminal filtration process, and the membrane aperture is 300-400nm; the secondary refining filtration adopts inorganic membrane pressure cross flow filtration technology, the filtration pressure is 200-300Kpa, and the membrane aperture is 40-50nm. Therefore, the residual refining agent AB in the secondary refining reaction liquid can be ensured to play a role in flocculation, and the full secondary refining reaction and the more reliable indexes of qualified salt water after secondary filtration can also be ensured. The system has high automation level and stable indexes, and can realize industrial continuous production.
Drawings
FIG. 1 is a schematic diagram of a vanadium chromium titanium waste salt refining system for chloralkali;
wherein, 1, a water distribution barrel; 2. a pipeline mixer; 3. a gas-liquid separator; 4. a salt dissolving pool; 5. a titanium filter screen; 6. a baffling groove; 7. a first-stage reaction tank; 8. a filtration head tank; 9. a primary filter; 10. a liquid inlet buffer tank; 11. a primary heat exchanger; 12. a secondary heat exchanger; 13. a chlorate decomposer; 14. a secondary reaction tank; 15. a coarse filter; 16. a secondary filter; 17. a primary slag discharging pool; 18. a first-stage plate-and-frame filter press; 19. a secondary slag discharging pool; 20. and (4) a secondary plate-and-frame filter press.
Detailed Description
The following detailed description of embodiments of the invention refers to the accompanying drawings.
In an embodiment of the invention, as shown in fig. 1, a system for refining vanadium, chromium and titanium waste salt for chlor-alkali is provided, which comprises a water distribution barrel 1, wherein the water distribution barrel 1 is sequentially connected with a pipeline mixer 2, a gas-liquid separator 3 and a salt dissolving tank 4, the salt dissolving tank 4 is connected with a titanium filter screen 5, the titanium filter screen 5 is sequentially connected with a baffle tank 6, a primary reaction tank 7, a filtration head tank 8, a primary filter 9 and a liquid inlet buffer tank 10, the primary filter 9 is further connected with the primary reaction tank 7, the liquid inlet buffer tank 10 is sequentially connected with a primary heat exchanger 11, a secondary heat exchanger 12, a chlorate decomposer 13 and a secondary reaction tank 14, the secondary heat exchanger 12 is further respectively connected with the baffle tank 6 and the secondary reaction tank 14, the chlorate decomposer 13 is further connected with the primary heat exchanger 11, the secondary reaction tank 14 is further connected with the liquid inlet buffer tank 10, the secondary reaction tank 14 is sequentially connected with a coarse filter 15 and a secondary filter 16, the coarse filter 15 and the secondary filter 16 are both connected with a secondary slag discharge tank 19, the secondary slag discharge tank 19 is connected with a secondary filter press 18, and a primary filter press 18 are both connected with a primary plate frame 17, and a secondary filter press filter 18.
Specifically, high-salinity wastewater containing vanadium, chromium and titanium (containing 100-150g/L of sodium chloride), press-filtered water or production water of a first-stage plate-and-frame filter press 18 and a second-stage plate-and-frame filter press 20 enter a water distribution barrel 1, and salt-containing wastewater in the water distribution barrel 1 is pumped into a salt dissolving pool 4 at a certain flow rate by a variable frequency pump; hydrochloric acid is added into the salt-containing wastewater before the salt evolution pond 4, the salt-containing wastewater is fully mixed and reacted in the pipeline mixer 2 and then enters the gas-liquid separator 3, the waste gas discharged from the top enters the waste gas treatment, and the liquid at the bottom flows into the salt evolution pond 4. The hydrochloric acid is added by adopting a variable frequency metering pump, and the pH value of the brine of the gas-liquid separator 3 is controlled to be 6.5-7.5.
Solid waste salt (sodium chloride is less than or equal to 93%) is added into the salt dissolving tank 4, the dilute brine is used for dissolving the solid waste salt to obtain saturated brine (sodium chloride is 290-310 g/L), the pH value is increased, a titanium filter screen 5 is arranged at the outlet of the salt dissolving tank 4, and the brine filtered from larger mechanical impurities automatically flows into a baffling tank 6.
Hydrochloric acid or low-pH salt water after chlorate decomposition and a refining agent AB are added into the baffling tank 6 at certain intervals; the refining agent AB is added by adopting a variable frequency metering pump, the adjustment is carried out according to the flow of the salt solution of the evolved salt pond 4, the addition of the hydrochloric acid is carried out by adopting the variable frequency metering pump, and the pH value of the salt solution which flows out of the baffling groove 6 and enters the primary reaction pond 7 is controlled to be 1.5-2.5.
In the first-stage reaction tank 7, a pH stabilizer is added, and the mixture is sufficiently stirred and mixed with the overflow brine of the filtration head tank 8 and the back flush brine of the first-stage filter 9. The brine in the first-stage reaction tank 7 is pumped into a filtering elevated tank 8 at a certain flow rate by a variable frequency pump. The pH stabilizer is added by a variable frequency metering pump, and the pH value of the brine entering the filtering head tank 8 is controlled to be 2.5-5.0.
The brine (overflowing to the first-stage reaction tank 7) of the filtering elevated tank 8 enters a first-stage filter 9, the first-stage filter 9 adopts an organic membrane micro-pressure terminal filtering process, the membrane pore size is 300-400nm, and the brine filtered by the organic membrane enters a liquid inlet buffer tank 10. After the organic membrane is filtered for a certain time, the back flushing and the slag discharging are automatically carried out. The backflushing salt water enters a first-stage reaction tank 7, and the first-stage slag discharging liquid enters a first-stage slag discharging tank 17.
The brine in the liquid inlet buffer tank 10 enters a chlorate decomposer 13 after being preheated by a primary heat exchanger 11 and a secondary heat exchanger 12 at a certain flow rate by adopting a variable frequency pump. The feed buffer tank 10 overflows the brine to the secondary reaction tank 14. The primary heat exchanger 11 is preheated by steam condensate water from the chlorate decomposer 13, and the steam condensate water enters the primary slag discharging pool 17. The secondary heat exchanger 12 is preheated with high temperature brine exiting the chlorate decomposer 13.
Before the saline water enters the chlorate decomposer 13, respectively adding hydrochloric acid and a chlorate decomposer, wherein the hydrochloric acid is added by adopting a variable frequency metering pump, and the pH value of the saline water entering the chlorate decomposer 13 is controlled to be 1.5-2.5; the chlorate decomposer is added by a variable frequency metering pump, and the addition amount is determined according to the flow rate of the brine entering the chlorate decomposer 13. In the chlorate decomposer 13, heating is performed with steam. The temperature of the brine of the chlorate decomposer 13 is controlled to be 80-95 ℃ by adopting a steam regulating valve.
The brine discharged from the chlorate decomposer 13 is cooled by the brine in the secondary heat exchanger 12 and then enters the secondary reaction tank 14, and a small amount of brine returns to the diversion tank 6 for adjusting the pH value of the brine in the diversion tank 6 and reducing the consumption of hydrochloric acid.
In the secondary reaction tank 14, the pH stabilizer is continuously added and mixed with the circulating brine of the secondary filter 16. The pH stabilizer is added by a variable frequency metering pump, and the pH value of the brine discharged from the secondary reaction tank 14 is controlled to be 7.0-9.0.
The salt water in the secondary reaction tank 14 enters a secondary filter 16 through a coarse filter 15 by using a variable frequency pump, and the pressure of the salt water entering the secondary filter 16 is controlled to be 200-300Kpa by using the variable frequency pump. The coarse filter 15 is filtered by a titanium mesh with the aperture of 0.6mm, and large particles are intercepted to protect a filter membrane of the secondary filter 16. The coarse filter 15 is used for automatically discharging slag regularly, and the slag discharging liquid enters the secondary slag discharging pool 19.
The secondary filter 16 adopts an inorganic membrane pressurized cross flow filtration process, the membrane aperture is 40-50nm, and most of the circulating liquid of the secondary filter 16 returns to the secondary reaction tank 14. The inorganic membrane pressure cross-flow filtration adopts continuous slag discharge, and the slag discharge liquid enters a secondary slag discharge tank 19. After filtering for a certain time by the inorganic membrane, the inorganic membrane is automatically back flushed by pure water. And controlling the flow of the brine filtered by the inorganic membrane to obtain qualified brine, and reusing the qualified brine in a chlor-alkali brine refining system to further remove other impurities.
The low pH value salt water in the first-stage deslagging pool 17 is pumped into a first-stage plate-and-frame filter press 18 by a pump for filter pressing, the filter pressing water is returned to the water distribution barrel 1, the higher pH value salt water in the second-stage deslagging pool 19 is pumped into the second-stage plate-and-frame filter press by the pump for filter pressing, and the filter pressing water is returned to the water distribution barrel 1. And (4) carrying out filter pressing on the salt mud obtained by the first-stage plate-and-frame filter press 18 and the second-stage plate-and-frame filter press 20 to form solid waste residues.
And the impurities are removed more thoroughly by utilizing different flow reflux regulation, the addition of a refining agent is saved, the steam consumption is reduced, and the production cost is reduced. The flow of the salt solution in the evolved salt pond 4 is slightly larger than that of the salt solution in the secondary filter 16 (a small amount of salt solution enters the slag pond through slag discharge), and the flow of the salt solution in the elevated tank of the primary filter 9 is 1.5-2.0 times of that of the salt solution in the evolved salt pond 4; the brine flow to the chlorate decomposer 13 is less than the brine flow (partial decomposition) of the secondary filter 16.
The process flow is as follows: after water is added into the high-salinity wastewater, dissolving vanadium, chromium and titanium solid waste salt to obtain saturated brine, adding hydrochloric acid, a refining agent AB and a pH value stabilizer, and performing primary refining reaction and filtration to obtain primary refined brine; adding hydrochloric acid and chlorate decomposer, and heating for chlorate decomposition reaction to obtain first-grade refined salt water of the low chlorate radical; and adding a pH value stabilizer, performing secondary refining reaction, and filtering to obtain qualified brine, and reusing the qualified brine in a chlor-alkali brine refining system to further remove other impurities.
While the embodiments of the invention have been described in detail in connection with the drawings, the invention should not be construed as limited to the scope of the patent. Various modifications and changes may be made by those skilled in the art without inventive work within the scope of the appended claims.
Claims (6)
1. The system is characterized by comprising a water distribution barrel, wherein the water distribution barrel is sequentially connected with a pipeline mixer, a gas-liquid separator and a salt dissolving tank, the salt dissolving tank is connected with a titanium filter screen, the titanium filter screen is sequentially connected with a baffling tank, a primary reaction tank, a filtering elevated tank, a primary filter and a liquid inlet buffer tank, the primary filter is further connected with the primary reaction tank, the liquid inlet buffer tank is sequentially connected with a primary heat exchanger, a secondary heat exchanger, a chlorate decomposer and a secondary reaction tank, the secondary heat exchanger is further respectively connected with the baffling tank and the secondary reaction tank, the chlorate decomposer is further connected with the primary heat exchanger, the secondary reaction tank is further connected with the liquid inlet buffer tank, the secondary reaction tank is sequentially connected with a coarse filter and a secondary filter, the coarse filter and the secondary filter are both connected with a secondary slag discharge tank, the secondary slag discharge tank is connected with a secondary plate frame filter press, the primary filter and the primary heat exchanger are both connected with a primary slag discharge tank, the primary slag discharge tank is connected with a primary plate frame filter press, and the secondary plate frame filter press are both connected with the water distribution barrel;
the using method of the vanadium, chromium and titanium waste salt refining system for chlor-alkali adopts a two-step method to remove vanadium, chromium and titanium, and comprises the steps of adding a refining agent AB and a pH stabilizer, and converting high-valence ions into low-valence ions or removing the high-valence ions by flocculation precipitation and filtration at a low pH value in the conversion process of the pH value from low to high; then, flocculating hydroxide precipitate is filtered and further removed under neutral or alkalescence; the refining agent AB is at least one of ferric nitrate, ferrous chloride, ferric trichloride, ferric sulfate, ferrous sulfate, ferric tribromide, ferrous bromide and ferric perchlorate;
the method specifically comprises the following steps: high-salinity wastewater and other salt dissolving water are mixed by a water distribution barrel to form salt dissolving water, hydrochloric acid is added to adjust the pH value, the salt dissolving water enters a salt dissolving tank to dissolve solid waste salt to obtain vanadium-chromium-titanium saturated salt water, then hydrochloric acid and a refining agent AB are added to be mixed, the mixed salt solution enters a primary reaction tank, a pH stabilizer is added to the primary reaction tank to maintain a low pH value, and the mixture is stirred and mixed to complete primary refining reaction; filtering the brine after the primary refining reaction by a primary filter, adding hydrochloric acid and a decomposing agent, then feeding into a chlorate decomposer, and heating by steam to maintain the reaction temperature to complete the decomposition of chlorate; the first-stage refined salt water with low chlorate ions enters a second-stage reaction tank, a pH stabilizer is continuously added into the second-stage reaction tank to maintain a high pH value, and the first-stage refined salt water and the second-stage refined salt water are mixed to complete a second-stage refining reaction; and filtering the brine after the secondary refining reaction by a secondary refining filter to obtain qualified brine, and entering a chlor-alkali brine refining system for continuously removing impurities.
2. The system of claim 1, wherein the pH of the brine is 6.5 to 7.5, the pH of the brine is 1.5 to 2.5 after the hydrochloric acid and the refining agent AB are added to the first-stage reaction tank, the pH of the brine is 2.5 to 5 after the pH stabilizer is added to the first-stage reaction tank, and the pH of the brine is 7 to 9 after the pH stabilizer is added to the second-stage reaction tank.
3. The system for refining waste vanadium chromium titanium salt for chlor-alkali of claim 1 wherein the reaction temperature in the chlorate decomposer is between 80 and 95 ℃ and the pH is between 1.5 and 2.5.
4. The system of claim 1, wherein the decomposition agent is at least one of sodium thiosulfate, formaldehyde, acetaldehyde and glyoxal.
5. The system for refining waste vanadium chromium titanium salt for chlor-alkali of claim 1 wherein the pH stabilizer comprises the following components in parts by mass: 5-7 parts of methyl alcohol amine, 1-3 parts of sodium hydroxide and 1-3 parts of sodium bicarbonate.
6. The system for refining vanadium, chromium and titanium waste salt for chlor-alkali as described in claim 1, wherein said qualified salt contains 290-310g/L sodium chloride, 0.01mg/L vanadium, chromium and titanium, 0.02mg/L other heavy metal ions and 5g/L chlorate.
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